EP0571358A1 - Process for the direct reduction of particulate material containing iron oxide - Google Patents

Process for the direct reduction of particulate material containing iron oxide Download PDF

Info

Publication number
EP0571358A1
EP0571358A1 EP19930890101 EP93890101A EP0571358A1 EP 0571358 A1 EP0571358 A1 EP 0571358A1 EP 19930890101 EP19930890101 EP 19930890101 EP 93890101 A EP93890101 A EP 93890101A EP 0571358 A1 EP0571358 A1 EP 0571358A1
Authority
EP
European Patent Office
Prior art keywords
fluidized bed
gas
reducing gas
bed reactor
reduction
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP19930890101
Other languages
German (de)
French (fr)
Other versions
EP0571358B1 (en
Inventor
Karl Dipl.-Ing. Czermak
Konstantin Dipl.-Ing. Milionis
Johannes Leopold Dipl.-Ing. Schenk
Siegfried Dipl.-Ing. Zeller
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Primetals Technologies Austria GmbH
Brifer International Ltd
Original Assignee
Voest Alpine Industrienlagenbau GmbH
Brifer International Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Voest Alpine Industrienlagenbau GmbH, Brifer International Ltd filed Critical Voest Alpine Industrienlagenbau GmbH
Publication of EP0571358A1 publication Critical patent/EP0571358A1/en
Application granted granted Critical
Publication of EP0571358B1 publication Critical patent/EP0571358B1/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B13/00—Obtaining lead
    • C22B13/02—Obtaining lead by dry processes
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/0033—In fluidised bed furnaces or apparatus containing a dispersion of the material
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B5/00—Making pig-iron in the blast furnace
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B5/00—General methods of reducing to metals
    • C22B5/02—Dry methods smelting of sulfides or formation of mattes
    • C22B5/12—Dry methods smelting of sulfides or formation of mattes by gases
    • C22B5/14—Dry methods smelting of sulfides or formation of mattes by gases fluidised material
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/10—Reduction of greenhouse gas [GHG] emissions
    • Y02P10/122—Reduction of greenhouse gas [GHG] emissions by capturing or storing CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/10—Reduction of greenhouse gas [GHG] emissions
    • Y02P10/134—Reduction of greenhouse gas [GHG] emissions by avoiding CO2, e.g. using hydrogen

Definitions

  • the invention relates to a process for the direct reduction of particulate iron oxide-containing material in a fluidized bed process, reformed gas being mixed with top gas formed in the direct reduction of the iron oxide-containing material and being fed as a reducing gas to a fluidized bed reduction zone, and a plant for carrying out the process.
  • a method of this type is known from US-A-5,082,251.
  • iron-rich fine ore is reduced in a system of fluidized bed reactors arranged in series with the aid of reducing gas under increased pressure.
  • the iron powder produced in this way is then subjected to hot or cold briquetting.
  • the reducing gas is generated by catalytic reforming of desulfurized and preheated natural gas with superheated steam in a conventional reformer furnace.
  • the reformed gas is then cooled to approx. 425 ° C in a heat exchanger.
  • This gas is mixed with the partially used reducing gas (top gas), heated to 850 ° C and reduces the fine ore in three stages (three reactors) in countercurrent.
  • the ore flow begins with drying and subsequent sieving. Then the ore gets into one Preheating reactor in which natural gas is burned. In three subsequent reactors, the fine ore is reduced under increased pressure.
  • the invention aims at avoiding these disadvantages and difficulties and has as its object to use the chemical potential of the reducing gas to reduce the energy requirement.
  • the task is to considerably reduce operating costs, in particular energy costs, for example by more than 30%.
  • both the top gas and the reformed gas are subjected to a CO2 wash and the reducing gas formed by mixing top gas and reformed gas to an H2 content in a range between 45 and 75%, preferably between 50 and 65%, and a CO content is set in a range between 10 and 20%.
  • the CO2 that forms does not lead to any disadvantage, since it is washed out in a CO2 scrubber through which the top gas is passed.
  • the CO content is capped at 20%. If the CO content is above this, difficulties can arise with the system; the pipes carrying this gas can be destroyed.
  • the H2 and CO content in the reducing gas is adjusted by operating a reformer, a reduced steam / natural gas ratio, which is preferably between 2.5 and 3.5, compared to conventional reformer operating modes. is observed. This makes it possible to keep the temperature in the reduction zone essentially constant.
  • the reducing gas is preferably adjusted to a CH4 content which is between 8 and 35%.
  • the direct reduction is carried out in a plurality of fluidized bed reduction zones connected in series, the reducing gas being passed in countercurrent to the particulate iron oxide-containing material from the reduction zone to the reduction zone and at least in the last fluidized bed reduction zone for the reducing gas Partial combustion by oxygen supply is subjected.
  • freshly formed reducing gas is also partly supplied directly to the individual fluidized bed reduction zones following the first fluidized bed reduction zone in the flow direction of the reducing gas, preferably in an amount of 5 to 15%. .
  • the direct reduction of the iron oxide-containing material is carried out in a plurality of fluidized-bed reduction zones connected in series, whereby for the preheating of the iron oxide-containing material in the first fluidized bed for this material, only reducing gas which is returned from the downstream fluidized-bed reduction zones is used. Only the sensible heat of the exhaust gas from the downstream reactors is used without burning a gas. This preheating can take place in one or more stages.
  • a further minimization of the energy requirement can be achieved according to a preferred embodiment in that a plurality of fluidized bed reactors are connected in series, the iron oxide-containing material from fluidized bed reactor to fluidized bed reactor via conveying lines in one direction and the reducing gas from fluidized bed reactor to fluidized bed reactor via connecting lines in the opposite Direction is guided, and wherein at least in the fluidized bed reactor last arranged in the reducing gas flow direction, in addition to the line supplying the reducing gas emerging from the upstream fluidized bed reactor, an oxygen supply line and optionally a natural gas supply line open out.
  • a constant temperature in all fluidized bed reactors at the same level is achieved according to a further embodiment in that a plurality of fluidized bed reactors are connected in series, the iron oxide-containing material from fluidized bed reactor to fluidized bed reactor via conveying lines in one direction and the reducing gas from fluidized bed reactor to fluidized bed reactor Connection lines in the is guided in the opposite direction, and the fluidized bed reactors are arranged in parallel with respect to the reduction gas flow next to the series connection with respect to an additional reduction gas supply line.
  • the plant according to the invention has four fluidized bed reactors 1 to 4 connected in series, material containing iron oxide, such as fine ore, being fed to the first fluidized bed reactor 1 via an ore feed line 5 and from fluidized bed reactor to fluidized bed reactor via feed lines 6 and the finished reduced material (sponge iron) in a briquetting plant 7 hot or cold briquetting. If necessary, the reduced iron is protected from reoxidation during the briquetting by an inert gas system, not shown.
  • material containing iron oxide such as fine ore
  • the fine ore Before the fine ore is introduced into the first fluidized bed reactor, it is subjected to an ore preparation, such as drying and sieving, which is not shown in detail.
  • Reducing gas is conducted in countercurrent to the ore flow from the fluidized bed reactor 4 to the fluidized bed reactor 3 to 1 and is discharged as top gas via a top gas discharge line 8 from the last fluidized bed reactor 1 in the gas flow direction and cooled and washed in a wet scrubber 9.
  • the reduction gas is produced by reforming natural gas supplied via line 11 and desulfurized in a desulfurization system 12 in a reformer 10.
  • the reformed gas formed from natural gas and steam consists essentially of H2, CO, CH4, H2O and CO2. This reformed gas is fed via the reformed gas line 13 to a plurality of heat exchangers 14, in which it is cooled to ambient temperature, as a result of which water is condensed out of the gas.
  • the reformed gas line 13 opens into the top gas discharge line 8 after the top gas has been compressed by means of a compressor 15.
  • the mixed gas thus formed is sent through a CO2 scrubber 16 and freed of CO2, and it is now available as a reducing gas.
  • This reducing gas is heated via the reducing gas supply line 17 in a gas heater 18 arranged downstream of the CO2 scrubber 16 to a reducing gas temperature of approximately 800 ° C. and fed to the first fluidized bed reactor 4 in the gas flow direction, where it is used with the fine ores to produce directly reduced iron reacts.
  • the fluidized bed reactors 4 to 1 are connected in series; the reducing gas passes through the connecting lines 19 from the fluidized bed reactor to the fluidized bed reactor.
  • top gas Part of the top gas is removed from the gas cycle 8, 17, 19 in order to avoid an enrichment of inert gases, such as N2.
  • the discharged top gas is fed via a branch line 20 to the gas heater 18 for heating the reducing gas and burned there. Any missing energy is supplemented by natural gas, which is supplied via the feed line 21.
  • the sensible heat of the reformed gas emerging from the reformer 10 and of the reformer smoke gases is used in a recuperator 22 to preheat the natural gas after passing through the desulfurization system 12, to generate the steam required for the reforming and the combustion air supplied to the gas heater via the line and if necessary, preheat the reducing gas.
  • the combustion air supplied to the reformer via line 24 is also preheated.
  • hot and fresh reducing gas is supplied to the fluidized bed reactors 1 to 3, which are arranged downstream of the first fluidized bed reactor 4 in the direction of reduction gas flow, via branch lines 27 fed directly, etc. in an amount of about 10% per fluidized bed reactor 1, 2 and 3.
  • the fluidized bed reactors 1 to 4 are therefore not only connected in series with regard to the reduction gas flow, but also connected in parallel as far as the supply of a small part of the reduction gas is concerned, whereas the fluidized bed reactors 1 to 4, as far as the discharge or forwarding of the reducing gas are concerned, are only connected in series in the illustrated embodiment.
  • the cold reformed gas 50,000 Nm3 / h
  • 145,000 Nm3 / h recirculated top gas led into the CO2 wash, where it was freed from the CO2.
  • the gas 182,000 Nm3 / h, had the following analysis: preferred ranges [%] [%] min. Max. CH4 16.29 8.00 - 35.00 CO2 0.10 0.10 - 3.50 CO 9.23 8.00 - 35.00 H2 57.92 45.00 - 75.00 H2O 1.52 1.50 - 5.00 N2 14.94 5.00 - 35.00
  • This gas was preheated to 800 ° C in a gas heater. About 5,500 Nm3 / h top gas and 4,600 Nm3 / h natural gas were used for this.
  • the hot briquetted iron had a degree of metallization (Fe met / Fe ges ) of 92%.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • Dispersion Chemistry (AREA)
  • Manufacture Of Iron (AREA)
  • Manufacture Of Metal Powder And Suspensions Thereof (AREA)
  • Blast Furnaces (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

In a process for the direct reduction of particulate iron oxide-containing material in the fluidised-bed process, reformed gas is mixed with the top gas resulting from the direct reduction of the iron oxide-containing material and is fed as reducing gas to a fluidised-bed reducing zone. To decrease the energy consumption and fully utilise the potential of the reducing gas, both the top gas and the reformed gas are subjected to a CO2 scrubbing and the reducing gas formed by mixing top gas and reformed gas is adjusted to an H2 content in a range between 45 and 75%, preferably between 50 and 65%, and a CO content in a range between 10 and 20%. <IMAGE>

Description

Die Erfindung betrifft ein Verfahren zur Direktreduktion von teilchenförmigem eisenoxidhältigen Material im Wirbelschichtverfahren, wobei reformiertes Gas mit bei der Direktreduktion des eisenoxidhältigen Materials entstehendem Topgas vermischt und als Reduktionsgas einer Wirbelschicht-Reduktionszone zugeführt wird, sowie eine Anlage zur Durchführung des Verfahrens.The invention relates to a process for the direct reduction of particulate iron oxide-containing material in a fluidized bed process, reformed gas being mixed with top gas formed in the direct reduction of the iron oxide-containing material and being fed as a reducing gas to a fluidized bed reduction zone, and a plant for carrying out the process.

Ein Verfahren dieser Art ist aus der US-A - 5,082,251 bekannt. Hierbei wird eisenreiches Feinerz in einem System von in Serie angeordneten Wirbelschichtreaktoren mit Hilfe von Reduktionsgas unter erhöhtem Druck reduziert. Das so erzeugte Eisenpulver wird anschließend einer Heiß- oder Kaltbrikettierung unterworfen.A method of this type is known from US-A-5,082,251. Here, iron-rich fine ore is reduced in a system of fluidized bed reactors arranged in series with the aid of reducing gas under increased pressure. The iron powder produced in this way is then subjected to hot or cold briquetting.

Das Reduktionsgas wird durch katalytische Reformierung von entschwefeltem und vorgewärmtem Erdgas mit überhitztem Wasserdampf in einem konventionellen Reformerofen erzeugt. Das reformierte Gas wird anschließend auf ca. 425°C in einem Wärmetauscher abgekühlt. Anschließend wird durch CO-Konvertierung mit Hilfe eines Eisenoxid-Katalysators der H₂-Anteil im Reduktionsgas nach folgender Gleichung erhöht:

        H₂O + CO = CO₂ + H₂

The reducing gas is generated by catalytic reforming of desulfurized and preheated natural gas with superheated steam in a conventional reformer furnace. The reformed gas is then cooled to approx. 425 ° C in a heat exchanger. Subsequently, the H₂ content in the reducing gas is increased by CO conversion using an iron oxide catalyst according to the following equation:

H₂O + CO = CO₂ + H₂

Anschließend wird das dabei entstehende sowie das vom Reformer stammende CO₂ in einem CO₂-Wäscher entfernt, so daß sich das Reduktionsgas aus über 90 % H₂, einem sehr geringen Anteil CO sowie CO₂, H₂O, N₂ und CH₄ zusammensetzt.Then the resulting and the CO₂ originating from the reformer is removed in a CO₂ scrubber, so that the reducing gas is composed of over 90% H₂, a very small proportion of CO and CO₂, H₂O, N₂ and CH₄.

Dieses Gas wird mit dem nur teilweise verbrauchten Reduktionsgas (Topgas) vermischt, auf 850°C erhitzt und reduziert in drei Stufen (drei Reaktoren) im Gegenstrom das Feinerz.This gas is mixed with the partially used reducing gas (top gas), heated to 850 ° C and reduces the fine ore in three stages (three reactors) in countercurrent.

Der Fluß des Erzes beginnt mit einer Trocknung und einer anschließenden Siebung. Sodann gelangt das Erz in einen Vorwärmereaktor, in dem Erdgas verbrannt wird. In drei folgenden Reaktoren wird das Feinerz unter erhöhtem Druck reduziert.The ore flow begins with drying and subsequent sieving. Then the ore gets into one Preheating reactor in which natural gas is burned. In three subsequent reactors, the fine ore is reduced under increased pressure.

Bei diesem Verfahren weist das Reduktionsgas einen sehr hohen Anteil an H₂ auf, so daß die Reduktion der Feinerze hier ausschließlich über die Reaktion:

        Fe₂O₃ + 3H₂ = 2Fe + 3H₂O - ΔH


erfolgt, die stark endotherm ist.In this process, the reducing gas has a very high proportion of H₂, so that the reduction of the fine ores here exclusively via the reaction:

Fe₂O₃ + 3H₂ = 2Fe + 3H₂O - ΔH


takes place, which is strongly endothermic.

Diese stark endotherme Reaktion würde eine wesentliche Temperaturabsenkung in den Reaktoren zur Folge haben. Um dies zu verhindern, ist man bei dem bekannten Verfahren gezwungen, die spezifische Reduktionsgasmenge pro t Eisenschwamm beträchtlich über die thermodynamisch erforderliche Mindestgasmenge zu erhöhen, so daß die Reaktionstemperatur im letzten Reaktor über 700°C liegt.This highly endothermic reaction would result in a significant drop in temperature in the reactors. In order to prevent this, the known process forces the specific amount of reducing gas per tonne of sponge iron to increase considerably above the thermodynamically required minimum amount of gas, so that the reaction temperature in the last reactor is above 700.degree.

Die Erfindung bezweckt die Vermeidung dieser Nachteile und Schwierigkeiten und stellt sich die Aufgabe, das chemische Potential des Reduktionsgases zur Senkung des Energiebedarfes heranzuziehen. Insbesondere ist die Aufgabe gestellt, die Betriebskosten, insbesondere die Energiekosten, beträchtlich zu reduzieren, beispielsweise um mehr als 30 %.The invention aims at avoiding these disadvantages and difficulties and has as its object to use the chemical potential of the reducing gas to reduce the energy requirement. In particular, the task is to considerably reduce operating costs, in particular energy costs, for example by more than 30%.

Diese Aufgabe wird erfindungsgemäß dadurch gelöst, daß sowohl das Topgas als auch das reformierte Gas einer CO₂-Wäsche unterzogen werden und das durch Mischen von Topgas und reformiertem Gas gebildete Reduktionsgas auf einen H₂-Gehalt in einem Bereich zwischen 45 und 75 %, vorzugsweise zwischen 50 und 65 %, und einen CO-Gehalt in einem Bereich zwischen 10 und 20 % eingestellt wird.This object is achieved in that both the top gas and the reformed gas are subjected to a CO₂ wash and the reducing gas formed by mixing top gas and reformed gas to an H₂ content in a range between 45 and 75%, preferably between 50 and 65%, and a CO content is set in a range between 10 and 20%.

Erfindungsgemäß erfolgt die Reduktion des Feinerzes nicht ausschließlich über die oben zum Stand der Technik beschriebene stark endotherme Reaktion mit H₂, sondern zusätzlich über die Reaktion

        Fe₂O₃ + 3CO = 2Fe + 3CO₂ + ΔH,


die exotherm ist. Das sich hierbei bildende CO₂ führt zu keinem Nachteil, da es in einem CO₂-Wäscher, durch den das Topgas durchgeleitet wird, ausgewaschen wird. Die Reaktion von CO mit H₂ nach der Gleichung

        CO + 3H₂ = CH₄ + H₂O


ist beim erfindungsgemäßen Verfahren nicht nachteilig, da das Methan nur in einer sehr geringen Konzentration gebildet wird, die keine Nachteile mit sich bringt.According to the invention, the reduction of the fine ore is carried out not only via the strongly endothermic reaction with H₂ described above in relation to the prior art, but also via the reaction

Fe₂O₃ + 3CO = 2Fe + 3CO₂ + ΔH,


which is exothermic. The CO₂ that forms does not lead to any disadvantage, since it is washed out in a CO₂ scrubber through which the top gas is passed. The reaction of CO with H₂ according to the equation

CO + 3H₂ = CH₄ + H₂O


is not disadvantageous in the method according to the invention, since the methane is only formed in a very low concentration which has no disadvantages.

Weiters ist es wesentlich, daß der CO-Gehalt mit 20 % nach oben begrenzt ist. Liegt der CO-Gehalt darüber, kann es zu Schwierigkeiten bei der Anlage kommen; es kann zu einer Zerstörung der dieses Gas leitenden Rohre kommen.Furthermore, it is essential that the CO content is capped at 20%. If the CO content is above this, difficulties can arise with the system; the pipes carrying this gas can be destroyed.

Durch die erfindungsgemaße CO₂-Wäsche des Topgases gemeinsam mit dem reformierten Gas gelingt es, den CO-Gehalt in einfacher Weise zu optimieren, nämlich dahingehend, daß eine Reaktion mit CO stattfindet, also eine Neutralhaltung der Energiebilanz (gegenüber der Reaktion mit H₂, die endotherm ist) möglich ist, jedoch eine Zerstörung der das Gas leitenden Rohre zuverlässig verhindert wird.Due to the inventive CO₂ scrubbing of the top gas together with the reformed gas, it is possible to optimize the CO content in a simple manner, namely in that a reaction with CO takes place, that is to say the energy balance is kept neutral (compared with the reaction with H₂, which is endothermic is possible, but destruction of the gas-conducting pipes is reliably prevented.

Aus der DE-A - 25 26 737 ist ein Verfahren gemäß dem Oberbegriff bekannt, bei dem jedoch Methan mit Sauerstoff in den Reaktorbehälter eingeleitet wird. Die Reduktionsgaserzeugung findet erst im Inneren des Reaktors, dem über eine separate Leitung einer CO₂-Wäsche unterworfenes Topgas zugeleitet wird, statt. Der CO-Gehalt liegt zwischen 31,6 % in der ersten Reaktionsstufe und 18,3 % in der letzten Reaktionsstufe. Er liegt somit im Durchschnitt weit über dem beanspruchten Maximal-Bereich.From DE-A - 25 26 737 a method according to the preamble is known, in which, however, methane with oxygen is introduced into the reactor vessel. The reduction gas generation takes place only in the interior of the reactor, to which top gas subjected to CO₂ scrubbing is fed via a separate line. The CO content is between 31.6% in the first reaction stage and 18.3% in the last reaction stage. It is therefore on average well above the maximum range claimed.

Gemäß einer bevorzugten Ausführungsform erfolgt erfindungsgemäß das Einstellen des H₂- und des CO-Gehaltes im Reduktionsgas durch die Betriebsweise eines Reformers, wobei gegenüber herkömmlichen Reformer-Betriebsweisen ein reduziertes Dampf/Erdgas-Verhältnis, das vorzugsweise zwischen 2,5 und 3,5 liegt, eingehalten wird. Hierdurch gelingt es, die Temperatur in der Reduktionszone im wesentlichen konstant zu halten.According to a preferred embodiment, according to the invention, the H₂ and CO content in the reducing gas is adjusted by operating a reformer, a reduced steam / natural gas ratio, which is preferably between 2.5 and 3.5, compared to conventional reformer operating modes. is observed. This makes it possible to keep the temperature in the reduction zone essentially constant.

Vorzugsweise wird das Reduktionsgas auf einen CH₄-Gehalt, der zwischen 8 und 35 % liegt, eingestellt.The reducing gas is preferably adjusted to a CH₄ content which is between 8 and 35%.

Zur Minimierung des Energiebedarfes wird gemäß einer bevorzugten Ausführungsform die Direktreduktion in mehreren in Serie hintereinander geschalteten Wirbelschicht-Reduktionszonen durchgeführt, wobei das Reduktionsgas im Gegenstrom zu dem teilchenförmigen eisenoxidhältigen Material von Reduktionszone zu Reduktionszone geführt wird und zumindest in der für das Reduktionsgas letzten Wirbelschicht-Reduktionszone einer Teilverbrennung durch Sauerstoffzufuhr unterzogen wird.In order to minimize the energy requirement, according to a preferred embodiment, the direct reduction is carried out in a plurality of fluidized bed reduction zones connected in series, the reducing gas being passed in countercurrent to the particulate iron oxide-containing material from the reduction zone to the reduction zone and at least in the last fluidized bed reduction zone for the reducing gas Partial combustion by oxygen supply is subjected.

Um in allen Wirbelschicht-Reduktionszonen eine etwa gleich hohe konstante Temperatur einzustellen, wird vorteilhaft frisch gebildetes Reduktionsgas zum Teil den der in Reduktionsgas-Strömungsrichtung ersten Wirbelschicht-Reduktionszone folgenden einzelnen Wirbelschicht-Reduktionszonen zusätzlich jeweils direkt zugeführt, vorzugsweise in einer Menge von 5 bis 15 %.In order to set an approximately equally high constant temperature in all fluidized bed reduction zones, it is advantageous if freshly formed reducing gas is also partly supplied directly to the individual fluidized bed reduction zones following the first fluidized bed reduction zone in the flow direction of the reducing gas, preferably in an amount of 5 to 15%. .

Gemäß einer bevorzugten Variante wird die Direktreduktion des eisenoxidhältigen Materials in mehreren in Serie hintereinander geschalteten Wirbelschicht-Reduktionszonen durchgeführt, wobei zur Vorwärmung des eisenoxidhältigen Materials in der für dieses Material ersten Wirbelschicht ausschließlich aus den nachgeordneten Wirbelschicht-Reduktionszonen rückgeführtes Reduktionsgas verwendet wird. Hierbei wird ausschließlich die fühlbare Wärme des Abgases aus den nachgeordneten Reaktoren ohne Verbrennung eines Gases ausgenutzt. Diese Vorwärmung kann ein- oder mehrstufig stattfinden.According to a preferred variant, the direct reduction of the iron oxide-containing material is carried out in a plurality of fluidized-bed reduction zones connected in series, whereby for the preheating of the iron oxide-containing material in the first fluidized bed for this material, only reducing gas which is returned from the downstream fluidized-bed reduction zones is used. Only the sensible heat of the exhaust gas from the downstream reactors is used without burning a gas. This preheating can take place in one or more stages.

Eine Anlage zur Durchführung des Verfahrens mit mindestens einem Wirbelschichtreaktor zur Aufnahme des eisenoxidhältigen Materials, einer Reduktionsgas-Zuleitung zu diesem Wirbelschichtreaktor und einer das sich bei der Reduktion bildende Topgas vom Wirbelschichtreaktor abführenden Topgas-Ableitung, mit einem Reformer, einer vom Reformer ausgehenden Reformgasleitung, die mit der Topgasleitung zusammenmündet, wobei das aus reformiertem Gas und Topgas gebildete Reduktionsgas über die Reduktionsgas-Zuleitung in den Wirbelschichtreaktor gelangt, und mit einem CO₂-Wäscher, ist dadurch gekennzeichnet, daß sowohl die Reformgasleitung als auch die Topgas-Ableitung in den CO₂-Wäscher münden und die Reduktionsgas-Zuleitung vom CO₂-Wäscher zum Wirbelschichtreaktor führt.A system for carrying out the process with at least one fluidized bed reactor for receiving the iron oxide-containing material, a reducing gas feed line to this fluidized bed reactor and a top gas discharge leading from the fluidized bed reactor during the reduction, with a reformer, a reformed gas line starting from the reformer, the merges with the top gas line, the reducing gas formed from reformed gas and top gas passing through the reducing gas feed line into the fluidized bed reactor, and with a CO₂ scrubber, is characterized in that both the reform gas line and the top gas discharge into the CO₂ scrubber flow and the reducing gas supply line from the CO₂ scrubber leads to the fluidized bed reactor.

Eine weitere Minimierung des Energiebedarfes läßt sich nach einer bevorzugten Ausführungsform dadurch erzielen, daß eine Mehrzahl von Wirbelschichtreaktoren hintereinander in Serie geschaltet sind, wobei das eisenoxidhältige Material von Wirbelschichtreaktor zu Wirbelschichtreaktor über Förderleitungen in einer Richtung und das Reduktionsgas von Wirbelschichtreaktor zu Wirbelschichtreaktor über Verbindungsleitungen in die entgegengesetzte Richtung geführt ist, und wobei zumindest in den in Reduktionsgas-Strömungsrichtung letztgeordneten Wirbelschichtreaktor zusätzlich zu der das aus dem vorgeordneten Wirbelschichtreaktor austretende Reduktionsgas zuführenden Leitung eine Sauerstoff-Zuführungsleitung und gegebenenfalls eine Erdgas-Zuführungsleitung münden.A further minimization of the energy requirement can be achieved according to a preferred embodiment in that a plurality of fluidized bed reactors are connected in series, the iron oxide-containing material from fluidized bed reactor to fluidized bed reactor via conveying lines in one direction and the reducing gas from fluidized bed reactor to fluidized bed reactor via connecting lines in the opposite Direction is guided, and wherein at least in the fluidized bed reactor last arranged in the reducing gas flow direction, in addition to the line supplying the reducing gas emerging from the upstream fluidized bed reactor, an oxygen supply line and optionally a natural gas supply line open out.

Eine Konstanthaltung der Temperaturen in sämtlichen Wirbelschichtreaktoren in gleicher Höhe wird nach einer weiteren Ausführungsform dadurch erzielt, daß eine Mehrzahl von Wirbelschichtreaktoren hintereinander in Serie geschaltet sind, wobei das eisenoxidhältige Material von Wirbelschichtreaktor zu Wirbelschichtreaktor über Förderleitungen in einer Richtung und das Reduktionsgas von Wirbelschichtreaktor zu Wirbelschichtreaktor über Verbindungsleitungen in die entgegengesetzte Richtung geführt ist, und wobei die Wirbelschichtreaktoren hinsichtlich der Reduktionsgasführung neben der Serienschaltung in bezug auf eine zusätzliche Reduktionsgaszuleitung in Parallelschaltung angeordnet sind.A constant temperature in all fluidized bed reactors at the same level is achieved according to a further embodiment in that a plurality of fluidized bed reactors are connected in series, the iron oxide-containing material from fluidized bed reactor to fluidized bed reactor via conveying lines in one direction and the reducing gas from fluidized bed reactor to fluidized bed reactor Connection lines in the is guided in the opposite direction, and the fluidized bed reactors are arranged in parallel with respect to the reduction gas flow next to the series connection with respect to an additional reduction gas supply line.

Die Erfindung ist nachfolgend anhand der Zeichnung, die ein Verfahrensschema nach einer bevorzugten Ausführungsform zeigt, näher erläutert.The invention is explained in more detail below with reference to the drawing, which shows a process diagram according to a preferred embodiment.

Die erfindungsgemäße Anlage weist vier in Serie hintereinander geschaltete Wirbelschichtreaktoren 1 bis 4 auf, wobei eisenoxidhältiges Material, wie Feinerz, über eine Erzzuleitung 5 dem ersten Wirbelschichtreaktor 1 und von Wirbelschichtreaktor zu Wirbelschichtreaktor über Förderleitungen 6 geleitet und das fertig reduzierte Material (Eisenschwamm) in einer Brikettieranlage 7 heiß- oder kaltbrikettiert wird. Erforderlichenfalls wird das reduzierte Eisen vor Reoxidation während der Brikettierung durch ein nicht dargestelltes Inertgas-System geschützt.The plant according to the invention has four fluidized bed reactors 1 to 4 connected in series, material containing iron oxide, such as fine ore, being fed to the first fluidized bed reactor 1 via an ore feed line 5 and from fluidized bed reactor to fluidized bed reactor via feed lines 6 and the finished reduced material (sponge iron) in a briquetting plant 7 hot or cold briquetting. If necessary, the reduced iron is protected from reoxidation during the briquetting by an inert gas system, not shown.

Vor Einleitung des Feinerzes in den ersten Wirbelschichtreaktor wird es einer Erzvorbereitung, wie einer Trocknung und einem Sieben, unterzogen, die nicht näher dargestellt ist.Before the fine ore is introduced into the first fluidized bed reactor, it is subjected to an ore preparation, such as drying and sieving, which is not shown in detail.

Reduktionsgas wird im Gegenstrom zum Erzdurchfluß von Wirbelschichtreaktor 4 zu Wirbelschichtreaktor 3 bis 1 geführt und als Topgas über eine Topgas-Ableitung 8 aus dem in Gasströmungsrichtung letzten Wirbelschichtreaktor 1 abgeleitet und in einem Naßwäscher 9 gekühlt und gewaschen. Die Herstellung des Reduktionsgases erfolgt durch Reformieren von über die Leitung 11 zugeführtem und in einer Entschwefelungsanlage 12 entschwefeltem Erdgas in einem Reformer 10. Das aus Erdgas und Dampf gebildete reformierte Gas besteht im wesentlichen aus H₂, CO, CH₄, H₂O und CO₂. Dieses reformierte Gas wird über die Reformgasleitung 13 mehreren Wärmetauschern 14 zugeleitet, in denen es auf Umgebungstemperatur abgekühlt wird, wodurch Wasser aus dem Gas auskondensiert wird.Reducing gas is conducted in countercurrent to the ore flow from the fluidized bed reactor 4 to the fluidized bed reactor 3 to 1 and is discharged as top gas via a top gas discharge line 8 from the last fluidized bed reactor 1 in the gas flow direction and cooled and washed in a wet scrubber 9. The reduction gas is produced by reforming natural gas supplied via line 11 and desulfurized in a desulfurization system 12 in a reformer 10. The reformed gas formed from natural gas and steam consists essentially of H₂, CO, CH₄, H₂O and CO₂. This reformed gas is fed via the reformed gas line 13 to a plurality of heat exchangers 14, in which it is cooled to ambient temperature, as a result of which water is condensed out of the gas.

Die Reformgasleitung 13 mündet in die Topgas-Ableitung 8, nachdem das Topgas mittels eines Kompressors 15 verdichtet wurde. Das so sich bildende Mischgas wird durch einen CO₂- Wäscher 16 hindurchgeschickt und von CO₂ befreit, und es steht nunmehr als Reduktionsgas zur Verfügung. Dieses Reduktionsgas wird über die Reduktionsgas-Zuleitung 17 in einem dem CO₂- Wäscher 16 nachgeordneten Gaserhitzer 18 auf eine Reduktionsgas-Temperatur von etwa 800°C erhitzt und dem in Gas-Durchflußrichtung ersten Wirbelschichtreaktor 4 zugeführt, wo es mit den Feinerzen zur Erzeugung von direkt reduziertem Eisen reagiert. Die Wirbelschichtreaktoren 4 bis 1 sind in Serie geschaltet; das Reduktionsgas gelangt über die Verbindungsleitungen 19 von Wirbelschichtreaktor zu Wirbelschichtreaktor.The reformed gas line 13 opens into the top gas discharge line 8 after the top gas has been compressed by means of a compressor 15. The mixed gas thus formed is sent through a CO₂ scrubber 16 and freed of CO₂, and it is now available as a reducing gas. This reducing gas is heated via the reducing gas supply line 17 in a gas heater 18 arranged downstream of the CO₂ scrubber 16 to a reducing gas temperature of approximately 800 ° C. and fed to the first fluidized bed reactor 4 in the gas flow direction, where it is used with the fine ores to produce directly reduced iron reacts. The fluidized bed reactors 4 to 1 are connected in series; the reducing gas passes through the connecting lines 19 from the fluidized bed reactor to the fluidized bed reactor.

Ein Teil des Topgases wird aus dem Gas-Kreislauf 8, 17, 19 ausgeschleust, um eine Anreicherung von Inertgasen, wie N₂, zu vermeiden. Das ausgeschleuste Topgas wird über eine Zweigleitung 20 dem Gaserhitzer 18 zur Erwärmung des Reduktionsgases zugeführt und dort verbrannt. Eventuell fehlende Energie wird durch Erdgas, welches über die Zuleitung 21 zugeführt wird, ergänzt.Part of the top gas is removed from the gas cycle 8, 17, 19 in order to avoid an enrichment of inert gases, such as N₂. The discharged top gas is fed via a branch line 20 to the gas heater 18 for heating the reducing gas and burned there. Any missing energy is supplemented by natural gas, which is supplied via the feed line 21.

Die fühlbare Wärme des aus dem Reformer 10 austretenden reformierten Gases sowie der Reformerrauchgase wird in einem Rekuperator 22 genutzt, um das Erdgas nach Durchlauf durch die Entschwefelungsanlage 12 vorzuwärmen, den für die Reformierung benötigten Dampf zu erzeugen sowie die dem Gaserhitzer über die Leitung zugeführte Verbrennungsluft sowie gegebenenfalls auch das Reduktionsgas vorzuwärmen. Die dem Reformer über die Leitung 24 zugeführte Verbrennungsluft wird ebenfalls vorgewärmt.The sensible heat of the reformed gas emerging from the reformer 10 and of the reformer smoke gases is used in a recuperator 22 to preheat the natural gas after passing through the desulfurization system 12, to generate the steam required for the reforming and the combustion air supplied to the gas heater via the line and if necessary, preheat the reducing gas. The combustion air supplied to the reformer via line 24 is also preheated.

Um eine Temperaturabsenkung im in Erzdurchlaufrichtung ersten Wirbelschichtreaktor 1 zu vermeiden, kann es vorteilhaft sein, einen Teil des aus dem zweiten Wirbelschichtreaktor 2 austretenden Reduktionsgases im ersten Wirbelschichtreaktor zu verbrennen, zu welchem Zweck in den ersten Wirbelschichtreaktor eine Sauerstoff-Zuführungsleitung 25 und gegebenenfalls eine Erdgas-Zuführungsleitung 26 münden.In order to avoid a temperature drop in the first fluidized bed reactor 1 in the direction of ore flow, it can be advantageous to remove a part of the fluidized bed reactor 2 from the second to burn out emerging reducing gas in the first fluidized bed reactor, for which purpose an oxygen supply line 25 and optionally a natural gas supply line 26 open into the first fluidized bed reactor.

Um in sämtlichen Wirbelschichtreaktoren 1 bis 4 die Reaktionstemperatur auf gleicher Höhe konstant zu halten und hierdurch eine weitere Senkung des Energiebedarfes zu erzielen, wird heißes und frisches Reduktionsgas den Wirbelschichtreaktoren 1 bis 3, die dem in Reduktionsgas-Strömungsrichtung ersten Wirbelschichtreaktor 4 nachgeordnet sind, über Zweigleitungen 27 direkt zugeführt, u.zw. in einer Menge von etwa 10 % je Wirbelschichtreaktor 1, 2 und 3. Die Wirbelschichtreaktoren 1 bis 4 sind somit hinsichtlich der Reduktionsgasführung nicht nur in Serie, sondern, was die Zuführung eines geringen Teiles des Reduktionsgases betrifft, auch parallel geschaltet, wogegen die Wirbelschichtreaktoren 1 bis 4, was die Ab- bzw. Weiterleitung des Reduktionsgases betrifft, beim dargestellten Ausführungsbeispiel ausschließlich in Serie geschaltet sind.In order to keep the reaction temperature constant at the same level in all fluidized bed reactors 1 to 4 and thereby achieve a further reduction in the energy requirement, hot and fresh reducing gas is supplied to the fluidized bed reactors 1 to 3, which are arranged downstream of the first fluidized bed reactor 4 in the direction of reduction gas flow, via branch lines 27 fed directly, etc. in an amount of about 10% per fluidized bed reactor 1, 2 and 3. The fluidized bed reactors 1 to 4 are therefore not only connected in series with regard to the reduction gas flow, but also connected in parallel as far as the supply of a small part of the reduction gas is concerned, whereas the fluidized bed reactors 1 to 4, as far as the discharge or forwarding of the reducing gas are concerned, are only connected in series in the illustrated embodiment.

Durch Verwendung von vier Wirbelschichtreaktoren 1 bis 4 zur Durchführung der Direktreduktion (unter Vermeidung eines Vorwärmreaktors) kommt es gegenüber dem Stand der Technik zu einer weiteren Senkung des Energiebedarfes und zu einer Minimierung von Staubverlusten.By using four fluidized bed reactors 1 to 4 to carry out the direct reduction (while avoiding a preheating reactor), the energy requirement is further reduced and dust losses are minimized compared to the prior art.

Beispiel:Example:

In einer der Zeichnung entsprechenden Anlage mit einer stündlichen Leistung von 70 t/h heißbrikettiertem Eisen wurden 100 t/h Feinerz, 12.200 Nm³/h Erdgas mit 43.300 Nm³/h Dampf zu 76.600 Nm³/h reformiertem Gas umgesetzt. Die Reformierungstemperatur betrug 830°C, der Druck 18,5 bar. Die für die Unterfeuerung des Reformers benötigte Erdgasmenge betrug 6.200 Nm³/h.In a plant corresponding to the drawing with an hourly output of 70 t / h hot briquetted iron, 100 t / h fine ore, 12,200 Nm³ / h natural gas with 43,300 Nm³ / h steam were converted to 76,600 Nm³ / h reformed gas. The reforming temperature was 830 ° C, the pressure 18.5 bar. The amount of natural gas required to fire the reformer was 6,200 Nm³ / h.

Die Analyse der betreffenden Gase und des Feinerzes lautete: Erdgas [%] Reformiertes Gas [%] Feinerz [%] CH₄ 83,4 2,30 Fe₂O₃ 93,94 CnHm 8,6 -- Gangart 1,84 CO₂ 8,0 10,70 Rest: Glühverluste CO -- 12,90 H₂ -- 68,90 O₂ -- -- N₂ -- 2,00 H₂S 20 ppm -- H₂O -- 3,20 The analysis of the gases and fine ore concerned was as follows: Natural gas [%] Reformed gas [%] Fine ore [%] CH₄ 83.4 2.30 Fe₂O₃ 93.94 C n H m 8.6 - Gait 1.84 CO₂ 8.0 10.70 Rest: loss on ignition CO - 12.90 H₂ - 68.90 O₂ - - N₂ - 2.00 H₂S 20 ppm - H₂O - 3.20

Das kalte reformierte Gas, 50.000 Nm³/h, wurde mit 145.000 Nm³/h rückgeführtem Topgas gemischt und in die CO₂-Wäsche geführt, wo es vom CO₂ befreit wurde. Das Gas, 182.000 Nm³/h, hatte folgende Analyse: bevorzugte Bereiche [%] [%] min. max. CH₄ 16,29 8,00 - 35,00 CO₂ 0,10 0,10 - 3,50 CO 9,23 8,00 - 35,00 H₂ 57,92 45,00 - 75,00 H₂O 1,52 1,50 - 5,00 N₂ 14,94 5,00 - 35,00 The cold reformed gas, 50,000 Nm³ / h, was mixed with 145,000 Nm³ / h recirculated top gas and led into the CO₂ wash, where it was freed from the CO₂. The gas, 182,000 Nm³ / h, had the following analysis: preferred ranges [%] [%] min. Max. CH₄ 16.29 8.00 - 35.00 CO₂ 0.10 0.10 - 3.50 CO 9.23 8.00 - 35.00 H₂ 57.92 45.00 - 75.00 H₂O 1.52 1.50 - 5.00 N₂ 14.94 5.00 - 35.00

Dieses Gas wurde in einem Gaserhitzer auf 800°C vorgewärmt. Dafür wurden ca. 5.500 Nm³/h Topgas und 4.600 Nm³/h Erdgas verbraucht.This gas was preheated to 800 ° C in a gas heater. About 5,500 Nm³ / h top gas and 4,600 Nm³ / h natural gas were used for this.

Die Analyse des Topgases lautete: [%] CH₄ 17,00 CO₂ 4,40 CO 4,90 H₂ 39,90 H₂O 18,90 N₂ 14,90 The analysis of the top gas was: [%] CH₄ 17.00 CO₂ 4.40 CO 4.90 H₂ 39.90 H₂O 18.90 N₂ 14.90

Das heißbrikettierte Eisen wies einen Metallisierungsgrad (Femet/Feges) von 92 % auf.The hot briquetted iron had a degree of metallization (Fe met / Fe ges ) of 92%.

Claims (10)

Verfahren zur Direktreduktion von teilchenförmigem eisenoxidhältigen Material im Wirbelschichtverfahren, wobei reformiertes Gas mit bei der Direktreduktion des eisenoxidhältigen Materials entstehendem Topgas vermischt und als Reduktionsgas einer Wirbelschicht-Reduktionszone zugeführt wird, dadurch gekennzeichnet, daß sowohl das Topgas als auch das reformierte Gas einer CO₂-Wäsche unterzogen werden und das durch Mischen von Topgas und reformiertem Gas gebildete Reduktionsgas auf einen H₂-Gehalt in einem Bereich zwischen 45 und 75 %, vorzugsweise zwischen 50 und 65 %, und einen CO-Gehalt in einem Bereich zwischen 10 und 20 % eingestellt wird.Process for the direct reduction of particulate iron oxide-containing material in a fluidized bed process, reformed gas being mixed with top gas formed in the direct reduction of the iron oxide-containing material and being fed as a reducing gas to a fluidized bed reduction zone, characterized in that both the top gas and the reformed gas are subjected to CO₂ scrubbing are and the reducing gas formed by mixing top gas and reformed gas to an H₂ content in a range between 45 and 75%, preferably between 50 and 65%, and a CO content in a range between 10 and 20%. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß das Einstellen des H₂- und des CO-Gehaltes im Reduktionsgas durch die Betriebsweise eines Reformers (10) erfolgt, wobei gegenüber herkömmlichen Reformer-Betriebsweisen ein reduziertes Dampf/Erdgas-Verhältnis, das vorzugsweise zwischen 2,5 und 3,5 liegt, eingehalten wird.A method according to claim 1, characterized in that the setting of the H₂ and CO content in the reducing gas is carried out by the operation of a reformer (10), a reduced steam / natural gas ratio, which is preferably between 2, compared to conventional reformer operations. 5 and 3.5 is observed. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, daß das Reduktionsgas auf einen CH₄-Gehalt, der zwischen 8 und 35 % liegt, eingestellt wird.A method according to claim 1 or 2, characterized in that the reducing gas is adjusted to a CH₄ content which is between 8 and 35%. Verfahren nach einem oder mehreren der Ansprüche 1 bis 3, dadurch gekennzeichnet, daß die Direktreduktion in mehreren in Serie hintereinander geschalteten Wirbelschicht-Reduktionszonen durchgeführt wird, wobei das Reduktionsgas im Gegenstrom zu dem teilchenförmigen eisenoxidhältigen Material von Reduktionszone zu Reduktionszone geführt wird und zumindest in der für das Reduktionsgas letzten Wirbelschicht-Reduktionszone einer Teilverbrennung durch Sauerstoffzufuhr unterzogen wird.Method according to one or more of claims 1 to 3, characterized in that the direct reduction is carried out in a plurality of fluidized bed reduction zones connected in series, the reducing gas being passed in countercurrent to the particulate iron oxide-containing material from the reduction zone to the reduction zone and at least in the the reducing gas in the last fluidized bed reduction zone is subjected to partial combustion by supplying oxygen. Verfahren nach einem oder mehreren der Ansprüche 1 bis 4, dadurch gekennzeichnet, daß frisch gebildetes Reduktionsgas zum Teil den der in Reduktionsgas-Strömungsrichtung ersten Wirbelschicht-Reduktionszone folgenden einzelnen Wirbelschicht-Reduktionszonen zusätzlich jeweils direkt zugeführt wird, vorzugsweise in einer Menge von 5 bis 15 %.Method according to one or more of claims 1 to 4, characterized in that freshly formed reducing gas in part, the individual fluidized bed reduction zones following the first fluidized bed reduction zone in the direction of reduction gas flow are additionally fed directly, preferably in an amount of 5 to 15%. Verfahren nach einem oder mehreren der Ansprüche 1 bis 3, dadurch gekennzeichnet, daß die Direktreduktion von eisenoxidhältigem Material in mehreren in Serie hintereinander geschalteten Wirbelschicht-Reduktionszonen durchgeführt wird, wobei zur Vorwärmung des eisenoxidhältigen Materials in der für das Material ersten Wirbelschicht ausschließlich aus den nachgeordneten Wirbelschicht-Reduktionszonen rückgeführtes Reduktionsgas verwendet wird.Method according to one or more of claims 1 to 3, characterized in that the direct reduction of iron oxide-containing material is carried out in a plurality of fluidized bed reduction zones connected in series, whereby for preheating the iron oxide-containing material in the first fluidized bed for the material exclusively from the downstream fluidized bed -Reduced reduction gas is used in reduction zones. Anlage zur Durchführung des Verfahrens nach einem oder mehreren der Ansprüche 1 bis 6, mit mindestens einem Wirbelschichtreaktor (1 bis 4) zur Aufnahme des eisenoxidhältigen Materials, einer Reduktionsgas-Zuleitung (17) zu diesem Wirbelschichtreaktor (1 bis 4) und einer das sich bei der Reduktion bildende Topgas vom Wirbelschichtreaktor (1) abführenden Topgas-Ableitung (8), mit einem Reformer (10), einer vom Reformer (10) ausgehenden Reformgasleitung (13), die mit der Topgasleitung (8) zusammenmündet, wobei das aus reformiertem Gas und Topgas gebildete Reduktionsgas über die Reduktionsgas-Zuleitung (17) in den Wirbelschichtreaktor (1 bis 4) gelangt, und mit einem CO₂-Wäscher (16), dadurch gekennzeichnet, daß sowohl die Reformgasleitung (13) als auch die Topgas-Ableitung (8) in den CO₂-Wäscher (16) münden und die Reduktionsgas-Zuleitung (17) vom CO₂-Wäscher (16) zum Wirbelschichtreaktor (1 bis 4) führt.Plant for carrying out the process according to one or more of claims 1 to 6, with at least one fluidized bed reactor (1 to 4) for receiving the iron oxide-containing material, a reducing gas feed line (17) to this fluidized bed reactor (1 to 4) and one of the two the reduction-forming top gas from the fluidized bed reactor (1) leading top gas discharge line (8), with a reformer (10), a reform gas line (13) emanating from the reformer (10), which opens out with the top gas line (8), which is made from reformed gas and top gas formed reducing gas passes through the reducing gas supply line (17) into the fluidized bed reactor (1 to 4), and with a CO₂ scrubber (16), characterized in that both the reformed gas line (13) and the top gas discharge line (8 ) open into the CO₂ scrubber (16) and the reducing gas feed line (17) from the CO₂ scrubber (16) leads to the fluidized bed reactor (1 to 4). Anlage nach Anspruch 7, dadurch gekennzeichnet, daß eine Mehrzahl von Wirbelschichtreaktoren (1 bis 4) hintereinander in Serie geschaltet sind, wobei das eisenoxidhältige Material von Wirbelschichtreaktor (1 bis 4) zu Wirbelschichtreaktor (1 bis 4) über Förderleitungen (6) in einer Richtung und das Reduktionsgas von Wirbelschichtreaktor (1 bis 4) zu Wirbelschichtreaktor (1 bis 4) über Verbindungsleitungen (19) in die entgegengesetzte Richtung geführt ist, und wobei zumindest in den in Reduktionsgas-Strömungsrichtung letztgeordneten Wirbelschichtreaktor (1) zusätzlich zu der das aus dem vorgeordneten Wirbelschichtreaktor austretende Reduktionsgas zuführenden Leitung (19) eine Sauerstoff-Zuführungsleitung (25) und gegebenenfalls eine Erdgas-Zuführungsleitung (26) münden.Plant according to claim 7, characterized in that a plurality of fluidized bed reactors (1 to 4) are connected in series, the material containing iron oxide from the fluidized bed reactor (1 to 4) to the fluidized bed reactor (1 to 4) via delivery lines (6) in one direction and the reducing gas is guided from the fluidized bed reactor (1 to 4) to the fluidized bed reactor (1 to 4) via connecting lines (19) in the opposite direction, and at least additionally in the fluidized bed reactor (1) which is the last one in the reducing gas flow direction An oxygen supply line (25) and optionally a natural gas supply line (26) open into the line (19) supplying the reducing gas emerging from the upstream fluidized bed reactor. Anlage nach Anspruch 7 oder 8, dadurch gekennzeichnet, daß eine Mehrzahl von Wirbelschichtreaktoren (1 bis 4) hintereinander in Serie geschaltet sind, wobei das eisenoxidhältige Material von Wirbelschichtreaktor (1 bis 4) zu Wirbelschichtreaktor (1 bis 4) über Förderleitungen (6) in einer Richtung und das Reduktionsgas von Wirbelschichtreaktor (1 bis 4) zu Wirbelschichtreaktor (1 bis 4) über Verbindungsleitungen (19) in die entgegengesetzte Richtung geführt ist, und wobei die Wirbelschichtreaktoren (1 bis 3) hinsichtlich der Reduktionsgasführung neben der Serienschaltung in bezug auf eine zusätzliche Reduktionsgaszuleitung in Parallelschaltung angeordnet sind.Plant according to claim 7 or 8, characterized in that a plurality of fluidized bed reactors (1 to 4) are connected in series, the iron oxide-containing material from fluidized bed reactor (1 to 4) to fluidized bed reactor (1 to 4) via delivery lines (6) in one direction and the reducing gas from the fluidized bed reactor (1 to 4) to the fluidized bed reactor (1 to 4) via connecting lines (19) in the opposite direction, and wherein the fluidized bed reactors (1 to 3) with respect to the reducing gas flow in addition to the series connection in relation to one additional reducing gas supply line are arranged in parallel. Anlage nach Anspruch 9, dadurch gekennzeichnet, daß vier Wirbelschicht-Reaktoren hintereinander in Serie geschaltet vorgesehen sind.Plant according to claim 9, characterized in that four fluidized bed reactors are provided connected in series.
EP93890101A 1992-05-22 1993-05-17 Process for the direct reduction of particulate material containing iron oxide Expired - Lifetime EP0571358B1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
AT1066/92 1992-05-22
AT106692 1992-05-22
AT0106692A AT402937B (en) 1992-05-22 1992-05-22 METHOD AND SYSTEM FOR DIRECTLY REDUCING PARTICULATE IRON OXIDE MATERIAL

Publications (2)

Publication Number Publication Date
EP0571358A1 true EP0571358A1 (en) 1993-11-24
EP0571358B1 EP0571358B1 (en) 1999-06-30

Family

ID=3505867

Family Applications (1)

Application Number Title Priority Date Filing Date
EP93890101A Expired - Lifetime EP0571358B1 (en) 1992-05-22 1993-05-17 Process for the direct reduction of particulate material containing iron oxide

Country Status (15)

Country Link
US (1) US5439504A (en)
EP (1) EP0571358B1 (en)
JP (1) JP2768888B2 (en)
KR (1) KR960008723B1 (en)
AT (1) AT402937B (en)
AU (1) AU669518B2 (en)
BR (1) BR9302014A (en)
CA (1) CA2096805C (en)
DE (1) DE59309667D1 (en)
DZ (1) DZ1692A1 (en)
EG (1) EG20233A (en)
MY (1) MY108789A (en)
RU (1) RU2078143C1 (en)
UA (1) UA27764C2 (en)
ZA (1) ZA933453B (en)

Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0673681A1 (en) * 1994-03-24 1995-09-27 VOEST-ALPINE Industrieanlagenbau GmbH (HRB 6375) Method of treating fine ore
DE19517766A1 (en) * 1994-08-12 1996-02-15 Midrex Int Bv Direct reduction system with circulating, fluidized bed
WO1997013878A1 (en) * 1995-10-10 1997-04-17 Voest-Alpine Industrieanlagenbau Gmbh Method of directly reducing a particulate iron oxide-containing material and plant for carrying out the method
WO1997013879A1 (en) * 1995-10-10 1997-04-17 Voest-Alpine Industrieanlagenbau Gmbh Method of directly reducing a particulate iron-containing material, and plant for carrying out the method
WO1997013880A1 (en) * 1995-10-10 1997-04-17 Voest-Alpine Industrieanlagenbau Gmbh Method of producing molten crude iron or molten crude steel, and plant for carrying out the method
AT402733B (en) * 1994-06-23 1997-08-25 Voest Alpine Ind Anlagen METHOD FOR DIRECTLY REDUCING IRON-OXIDATING MATERIAL
AT402938B (en) * 1994-06-23 1997-09-25 Voest Alpine Ind Anlagen METHOD AND SYSTEM FOR DIRECTLY REDUCING METHOD AND SYSTEM FOR DIRECTLY REDUCING MATERIAL IN IRON OXIDE MATERIAL IN IRON OXIDE
AT402825B (en) * 1994-06-23 1997-09-25 Voest Alpine Ind Anlagen METHOD FOR DIRECTLY REDUCING IRON-OXIDATING MATERIAL
US5674308A (en) * 1994-08-12 1997-10-07 Midrex International B.V. Rotterdam, Zurich Branch Spouted bed circulating fluidized bed direct reduction system and method
WO1997044495A1 (en) * 1996-05-17 1997-11-27 Voest-Alpine Industrieanlagenbau Gmbh Process for the treatment of particulate matter by fluidisation, and vessel with apparatus to carry out the treatment
WO1998020171A1 (en) * 1996-11-06 1998-05-14 Voest-Alpine Industrieanlagenbau Gmbh Process for producing sponge iron by direct reduction of iron oxide-containing materials
WO1999009220A1 (en) * 1997-08-18 1999-02-25 Voest-Alpine Industrieanlagenbau Gmbh Method and apparatus for the direct reduction of a material containing iron oxide in a particulate form
AT405057B (en) * 1994-09-27 1999-05-25 Voest Alpine Ind Anlagen METHOD FOR REDUCING OXIDE CONTAINING MATERIAL AND SYSTEM FOR IMPLEMENTING THE METHOD
US5997609A (en) * 1994-12-01 1999-12-07 Voest-Alpine Industrieanlagenbau Gmbh Sponge iron production process and plant
US6241801B1 (en) 1996-05-17 2001-06-05 Voest-Alpine Industrieanlagenbau Gmbh Method for treating particulate material in the fluidized bed method and vessel and plant for carrying out the method
EP1689892A1 (en) * 2003-12-05 2006-08-16 Posco An apparatus for manufacturing a molten iron directly using fine or lump coals and fine iron ores, the method thereof, the integrated steel mill using the same and the method thereof
US7597739B2 (en) 2001-09-27 2009-10-06 Voest-Alpine Industrieanlagenbau Gmbh & Co. Method for reducing a particulate material containing a metal, especially iron ore

Families Citing this family (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR970003636B1 (en) * 1994-12-31 1997-03-20 포항종합제철 주식회사 A furnace for reduction fine coal in the manufacture of iron melts
KR100213327B1 (en) * 1995-12-29 1999-08-02 이구택 Three-stage fluidized-bed reactor for the reduction of fine ore
AT405742B (en) * 1996-07-10 1999-11-25 Voest Alpine Ind Anlagen METHOD FOR PRODUCING LIQUID METAL AND SYSTEM FOR IMPLEMENTING THE METHOD
US5912400A (en) * 1997-12-02 1999-06-15 Brifer International Ltd. Method for reforming reducing gas in a fluidized bed process for reduction of ore
WO2002000944A1 (en) * 2000-06-28 2002-01-03 Voest-Alpine Industrieanlagenbau Gmbh & Co Method and device for directly reducing particulate oxide-containing ores
AT409387B (en) 2000-06-28 2002-07-25 Voest Alpine Ind Anlagen Process and installation for the gas reduction of particulate oxide-containing ores
US6478841B1 (en) 2001-09-12 2002-11-12 Techint Technologies Inc. Integrated mini-mill for iron and steel making
FR2883773B1 (en) * 2005-04-01 2007-05-11 Alstom Sa COMBUSTION DEVICE PRODUCING HYDROGEN WITH REUSE OF CO2 CAPTURE
JP5334240B2 (en) * 2008-06-30 2013-11-06 新日鐵住金株式会社 Method for producing reduced iron agglomerates for steelmaking
AT508523B1 (en) 2009-07-31 2011-04-15 Siemens Vai Metals Tech Gmbh REFORM GAS-BASED REDUCTION PROCESS AND DEVICE WITH DECARBONIZING THE COMBUSTION GAS FOR THE REFORMER
CN105492376A (en) 2013-07-22 2016-04-13 沙特基础工业公司 Use of top gas in direct reduction processes

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3193378A (en) * 1964-03-16 1965-07-06 Exxon Research Engineering Co Process for reduction of iron ore
DE2526737A1 (en) * 1974-06-17 1975-12-18 Centro Speriment Metallurg METHOD FOR REDUCING IRON ORE
DE2911692A1 (en) * 1979-03-24 1980-10-02 Metallgesellschaft Ag METHOD FOR PRODUCING REDUCING GAS FROM SOLID FUELS
US5082251A (en) * 1990-03-30 1992-01-21 Fior De Venezuela Plant and process for fluidized bed reduction of ore

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2752234A (en) * 1955-07-07 1956-06-26 United States Steel Corp Process for continuous gaseous reduction of iron ore in a fluidized bed system
US3684482A (en) * 1971-02-24 1972-08-15 Exxon Research Engineering Co Split feed to a fluidized iron ore reduction process
JPS5448622A (en) * 1977-09-27 1979-04-17 Kawasaki Steel Co Carbonndeposited reduced iron powder and method of making same
JPS5785912A (en) * 1980-11-18 1982-05-28 Ishikawajima Harima Heavy Ind Co Ltd Operating method for coal fluidized bed type reduction process
JPS5834114A (en) * 1981-08-21 1983-02-28 Kobe Steel Ltd Manufacture of reduced iron
JPS5834113A (en) * 1981-08-21 1983-02-28 Kobe Steel Ltd Manufacture of reduced iron

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3193378A (en) * 1964-03-16 1965-07-06 Exxon Research Engineering Co Process for reduction of iron ore
DE2526737A1 (en) * 1974-06-17 1975-12-18 Centro Speriment Metallurg METHOD FOR REDUCING IRON ORE
DE2911692A1 (en) * 1979-03-24 1980-10-02 Metallgesellschaft Ag METHOD FOR PRODUCING REDUCING GAS FROM SOLID FUELS
US5082251A (en) * 1990-03-30 1992-01-21 Fior De Venezuela Plant and process for fluidized bed reduction of ore

Cited By (32)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5676734A (en) * 1994-03-24 1997-10-14 Voest-Alpine Industrieanlagenbau Gmbh Method of treating fine ore
EP0673681A1 (en) * 1994-03-24 1995-09-27 VOEST-ALPINE Industrieanlagenbau GmbH (HRB 6375) Method of treating fine ore
US5858058A (en) * 1994-06-23 1999-01-12 Voest-Alpine Industrieanlagenbau Gmbh Process and plant for avoiding metal dusting in the direct reduction of iron-oxide-containing materials
US5855643A (en) * 1994-06-23 1999-01-05 Voest-Alpine Industrieanlagenbau Gmbh Direct reduction process for iron oxide-containing materials
US5871560A (en) * 1994-06-23 1999-02-16 Voest-Alpine Industrieanlagenbau Gmbh Process and plant for the direct reduction of iron-oxide-containing materials
AT402733B (en) * 1994-06-23 1997-08-25 Voest Alpine Ind Anlagen METHOD FOR DIRECTLY REDUCING IRON-OXIDATING MATERIAL
AT402938B (en) * 1994-06-23 1997-09-25 Voest Alpine Ind Anlagen METHOD AND SYSTEM FOR DIRECTLY REDUCING METHOD AND SYSTEM FOR DIRECTLY REDUCING MATERIAL IN IRON OXIDE MATERIAL IN IRON OXIDE
AT402825B (en) * 1994-06-23 1997-09-25 Voest Alpine Ind Anlagen METHOD FOR DIRECTLY REDUCING IRON-OXIDATING MATERIAL
DE19517766A1 (en) * 1994-08-12 1996-02-15 Midrex Int Bv Direct reduction system with circulating, fluidized bed
US5674308A (en) * 1994-08-12 1997-10-07 Midrex International B.V. Rotterdam, Zurich Branch Spouted bed circulating fluidized bed direct reduction system and method
US5529291A (en) * 1994-08-12 1996-06-25 Midrex International B.V. Rotterdam, Zurich Branch Circulating fluidized bed direct reduction system
AT405057B (en) * 1994-09-27 1999-05-25 Voest Alpine Ind Anlagen METHOD FOR REDUCING OXIDE CONTAINING MATERIAL AND SYSTEM FOR IMPLEMENTING THE METHOD
US5997609A (en) * 1994-12-01 1999-12-07 Voest-Alpine Industrieanlagenbau Gmbh Sponge iron production process and plant
WO1997013879A1 (en) * 1995-10-10 1997-04-17 Voest-Alpine Industrieanlagenbau Gmbh Method of directly reducing a particulate iron-containing material, and plant for carrying out the method
AU695624B2 (en) * 1995-10-10 1998-08-20 Pohang Iron & Steel Co., Ltd. Process for producing molten pig iron or liquid steel preproducts and plant for carrying out the process
WO1997013880A1 (en) * 1995-10-10 1997-04-17 Voest-Alpine Industrieanlagenbau Gmbh Method of producing molten crude iron or molten crude steel, and plant for carrying out the method
WO1997013878A1 (en) * 1995-10-10 1997-04-17 Voest-Alpine Industrieanlagenbau Gmbh Method of directly reducing a particulate iron oxide-containing material and plant for carrying out the method
US5833734A (en) * 1995-10-10 1998-11-10 Voest-Alpine Industrieanlagenbau Gmbh Process for the direct reduction of particulate iron-containing material and a plant for carrying out the process
US5961690A (en) * 1995-10-10 1999-10-05 Voest-Alpine Industrieanlagenbau Gmbh Process for producing molten pig iron of liquid steel preproducts and plant for carrying out the process
US6241801B1 (en) 1996-05-17 2001-06-05 Voest-Alpine Industrieanlagenbau Gmbh Method for treating particulate material in the fluidized bed method and vessel and plant for carrying out the method
AT405522B (en) * 1996-05-17 1999-09-27 Voest Alpine Ind Anlagen METHOD FOR TREATING PARTICLE-SHAPED MATERIALS IN A FLUID BED LAYER METHOD, AND VESSEL AND SYSTEM FOR IMPLEMENTING THE METHOD
WO1997044495A1 (en) * 1996-05-17 1997-11-27 Voest-Alpine Industrieanlagenbau Gmbh Process for the treatment of particulate matter by fluidisation, and vessel with apparatus to carry out the treatment
AU728390B2 (en) * 1996-05-17 2001-01-11 Voest-Alpine Industrieanlagenbau Gmbh Method for treating particulate material in the fluidized bed method and vessel and plant for carrying out the method
WO1998020171A1 (en) * 1996-11-06 1998-05-14 Voest-Alpine Industrieanlagenbau Gmbh Process for producing sponge iron by direct reduction of iron oxide-containing materials
US6143053A (en) * 1996-11-06 2000-11-07 Voest-Alpine Industrieanlagenbau Gmbh Process for producing sponge iron by direct reduction of iron-oxide-containing material
WO1999009220A1 (en) * 1997-08-18 1999-02-25 Voest-Alpine Industrieanlagenbau Gmbh Method and apparatus for the direct reduction of a material containing iron oxide in a particulate form
US6336954B1 (en) 1997-08-18 2002-01-08 Voest-Alpine Industrieanlagenbau Gmbh Process and plant for the direct reduction of particulate iron-oxide-containing material
AU743694B2 (en) * 1997-08-18 2002-01-31 Brifer International Ltd. Method and apparatus for the direct reduction of a material containing iron oxide in a particulate form
US6569377B2 (en) 1997-08-18 2003-05-27 Voest-Alpine Industrieanlagenbau Gmbh Plant for the direct reduction of particulate iron-oxide-containing material
US7597739B2 (en) 2001-09-27 2009-10-06 Voest-Alpine Industrieanlagenbau Gmbh & Co. Method for reducing a particulate material containing a metal, especially iron ore
EP1689892A1 (en) * 2003-12-05 2006-08-16 Posco An apparatus for manufacturing a molten iron directly using fine or lump coals and fine iron ores, the method thereof, the integrated steel mill using the same and the method thereof
EP1689892A4 (en) * 2003-12-05 2008-03-19 Posco An apparatus for manufacturing a molten iron directly using fine or lump coals and fine iron ores, the method thereof, the integrated steel mill using the same and the method thereof

Also Published As

Publication number Publication date
JP2768888B2 (en) 1998-06-25
KR930023474A (en) 1993-12-18
RU2078143C1 (en) 1997-04-27
ATA106692A (en) 1997-02-15
JPH0681019A (en) 1994-03-22
EG20233A (en) 1998-05-31
KR960008723B1 (en) 1996-06-29
CA2096805C (en) 1999-03-02
DZ1692A1 (en) 2002-02-17
ZA933453B (en) 1994-06-15
UA27764C2 (en) 2000-10-16
EP0571358B1 (en) 1999-06-30
CA2096805A1 (en) 1993-11-23
MY108789A (en) 1996-11-30
US5439504A (en) 1995-08-08
BR9302014A (en) 1993-11-30
AU669518B2 (en) 1996-06-13
DE59309667D1 (en) 1999-08-05
AT402937B (en) 1997-09-25
AU3859493A (en) 1993-11-25

Similar Documents

Publication Publication Date Title
EP0571358A1 (en) Process for the direct reduction of particulate material containing iron oxide
EP0796348B1 (en) Method of directly reducing a particulate iron-containing material, and plant for carrying out the method
AT402825B (en) METHOD FOR DIRECTLY REDUCING IRON-OXIDATING MATERIAL
DE4025320C2 (en) Process and reduction shaft furnace for the direct reduction of iron-containing metal oxides
DD153701A5 (en) METHOD AND APPARATUS FOR REDUCING IRON OXIDE TO METALIZED IRON
EP2751294B1 (en) Method for treating waste gases from plants for pig iron production
AT406380B (en) METHOD FOR PRODUCING LIQUID GUT IRON OR LIQUID STEEL PRE-PRODUCTS AND SYSTEM FOR IMPLEMENTING THE METHOD
DE3202220A1 (en) PLANT FOR DIRECT REDUCTION FROM IRON OXIDE TO METALLIC IRON
EP0766748B1 (en) Direct reduction process for iron oxide-containing materials
EP0871782B1 (en) Process for producing sponge iron by direct reduction of iron oxide-containing materials
DE2407939B2 (en) Method and device for the gas reduction of classified iron ores
EP0804621B1 (en) Direct reduction process for iron oxide-containing materials
AT406379B (en) METHOD FOR DIRECTLY REDUCING PARTICULAR IRON-OXIDATED MATERIAL AND SYSTEM FOR IMPLEMENTING THE METHOD
DE2947128C2 (en) Process for the continuous generation of a high-temperature reducing gas
AT407879B (en) METHOD FOR DIRECTLY REDUCING IRON OXIDE MATERIALS
EP1294953B1 (en) Device for directly reducing ore fine and installation for carrying out said method
DE19748968C1 (en) Process for producing a mixture of iron carbide and granular, directly reduced iron
AT405652B (en) Process for direct reduction of particulate iron- containing material, and installation for carrying out the process
DE2164008B2 (en) Process for the production of reducing gas
DE19525270C2 (en) Process for the production of pig iron from iron oxides
AT409386B (en) Process and installation for the direct reduction of particulate oxide-containing ores
DE2526737C3 (en) Process for reducing iron ore
DE3145507A1 (en) Process for producing metal sponge and device for carrying out the process
WO2002000944A1 (en) Method and device for directly reducing particulate oxide-containing ores
DE2526737A1 (en) METHOD FOR REDUCING IRON ORE

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): DE GB IT LU SE

17P Request for examination filed

Effective date: 19931020

RIN1 Information on inventor provided before grant (corrected)

Inventor name: ZELLER, SIEGFRIED, DIPL.-ING.

Inventor name: SCHENK, JOHANNES LEOPOLD, DIPL.-ING.

Inventor name: MILIONIS, KONSTANTIN, DIPL.-ING.

Inventor name: CZERMAK, KARL, DIPL.-ING.

RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: BRIFER INTERNATIONAL LTD.

Owner name: VOEST-ALPINE INDUSTRIEANLAGENBAU GMBH

17Q First examination report despatched

Effective date: 19961219

RIN1 Information on inventor provided before grant (corrected)

Inventor name: WHIPP, ROY HUBERT JR.

Inventor name: ZELLER, SIEGFRIED, DIPL.-ING.

Inventor name: SCHENK, JOHANNES LEOPOLD, DIPL.-ING.

Inventor name: MILIONIS, KONSTANTIN, DIPL.-ING.

Inventor name: CZERMAK, KARL, DIPL.-ING.

GRAG Despatch of communication of intention to grant

Free format text: ORIGINAL CODE: EPIDOS AGRA

GRAG Despatch of communication of intention to grant

Free format text: ORIGINAL CODE: EPIDOS AGRA

GRAH Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOS IGRA

GRAH Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOS IGRA

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): DE GB IT LU SE

GBT Gb: translation of ep patent filed (gb section 77(6)(a)/1977)

Effective date: 19990630

REF Corresponds to:

Ref document number: 59309667

Country of ref document: DE

Date of ref document: 19990805

ITF It: translation for a ep patent filed

Owner name: INTERPATENT ST.TECN. BREV.

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LU

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20000517

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20000518

26N No opposition filed
EUG Se: european patent has lapsed

Ref document number: 93890101.4

REG Reference to a national code

Ref country code: GB

Ref legal event code: IF02

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 20020502

Year of fee payment: 10

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20030517

GBPC Gb: european patent ceased through non-payment of renewal fee

Effective date: 20030517

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: IT

Payment date: 20120529

Year of fee payment: 20

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 20120720

Year of fee payment: 20

REG Reference to a national code

Ref country code: DE

Ref legal event code: R071

Ref document number: 59309667

Country of ref document: DE

REG Reference to a national code

Ref country code: DE

Ref legal event code: R071

Ref document number: 59309667

Country of ref document: DE

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION

Effective date: 20130518